Method of producing gas and a dry residue by the reaction of a solid and a liquid



Feb, 25, 1941. I s L 2,233,108

NES METHOD OF PRODUCING GAS AND A DRY RESIDUE BY THE REACTION OF A SOLID AND A LIQUID Filed Oct. 1, 1936 3 Sheets-Sheet 1 INVENTORS CHARLES NESS HUGO v. KOJ'OLA ATTORNEY Feb. 25, 1941. c. NESS ETAL I 2,233,108

METHOD OF PRODUCING GAS AND A DRY RESIDUE BY THE REACTION OF A SOLID AND A LIQUID Filed Oct. 1, 1936 3 Sheets-Sheet 2 INVENTORS CHARLES NESS HUGO V. KOJ'O-LA ATTO R N EY Feba 25, 19-41. c, 555 ETAL 2,233,108

METHOD OF PRODUCING GAS AND A DRY RESIDUE BY THE REACTION OF A SOLID AND A LIQUID Filed Oct. 1, 1936 v 3 Sheets-Sheet 3 A INVENTORS CHARLES NESS HUGO V. KOJ'OLA 'TORNEY Patented Feb. 25, 1941 PATENT OFFICE 'METHOD or, rizionuomc REACTION or RESIDUE BYI'I'HE AND A LIQUID- Charles Ness and 1nd,, assignors Hugo V. to The PI'est-O-Lite Compan GAS m A par a sonm 1 Koiola, Indianapolis,

Inc, a corporation of New York Application October 1, 1936, Serial No. 103,526 20 (Cl. 48-216) This invention relates to a method of producing gas and a dry residue by the reaction of a solid with a liquid, and more particularly to the production of acetylene from calcium car- I bide and waterwith the formation of a substantially dry hydrated lime residue.

Generally, the object of the present invention is to provide an improved process-by which the generation of a gas and the productionof a substantially dry, commercially useful residue is accomplished as a result of a controlled reaction between a solid and a liquid in a relatively simple, safe, economical and effective manner for the production of commercial volumes of gas.

More specifically, objects of the invention are to provide a process of the character indicated by which calcium carbide is continuously and completely reacted to simultaneously produce acetylene and substantially dry calcium hydrate in commercial quantities; by which the heat of the reaction is effectively controlled and disobjects will become persed so that objectionable efiects of local high temperatures are avoided; which shall be inherently stable so that the quality of the residue product will be unaffected by minor variations in the supply of reactants; by which heavy impurities unavoidably introduced with the carbide and particles of unreacted carbide are prevented from passing out with, and contaminating the residue; by which water evaporated to absorb excess heat of the reaction, is prevented from unduly moistening the residue produced; by which calcium hydrate being produced is maintained in a free flowing,.- fluid-like condltion so that a classification and counterfiow'oi carbide and residue will occur to provide a more effective contact of carbidewith water which results in rapid rates of production with more effective control of temperature; and which shall be equally effective in the use of lump, dust, granular and run-of-crusher sizes of carbide.

These and other objects of the invention and the novel features thereof which achieve these evident from the following detailed description taken in connection with the accompanying drawings, in which:

Fig. 1 is an elevational view-partly in section of an apparatus for generating acetylene with the production of a substantially dry residue according to the present invention;

Fig. 2 is a similar view of another formof the apparatus for practicing the method of the present invention; r

Fig. 3 is a view of a section of the apparatus shown in Fig. 2,

taken on the lined-him Fig. 4 is an elevational view of the agitating device shown in Fig. 2.

Acetylene is commonly generated by feeding calcium carbide into abody of water, there being a suflicient quantity of water present so that the heat produced by the reaction between the water and carbide is absorbed by the excess water as sensible heat. The residue resulting from the reaction is then in the form of a sludge. The generation of acetylene mass of carbide has been found to be exceedingly dangerous unless the amount of carbide is very small and the rate of the reaction is controlled to be very slow so that the heat produced may be dissipated by conduction through mass. The useof the latter method of generation has therefore been limited to the production of very small quantities of gas such as for portable lamps and no attempt has been made in such cases to regulate the addition of water to obtain a dry residue.

To produce commercial quantities of acetylene and a substantially dry residue without encoun tering dangerously high temperatures, it has been proposed to adda sufllcient quantity of water to carbide to satisfy the requirement for complete reaction and an additional quantity just sufflcient to absorb the excess heat reaction by its evaporation and subject the reacting materials to mechanical stirring in a horizontal retort for a considerable period until the reaction is complete. The carbide and the residue are carried along through an extended substantially horizontal path through the retort and if the quantities of water and carbide have been proper proportion, a substantially dry residue may result at the discharge end of the retort. It is difllcult however to control the temperatures locally occurring in the retort-to within desired limitsand at the same residue that is either not too wet or that does not contain unspent carbide, for particles of carbide may be carried along to places where the surrounding material .is too dry to complete the reaction. carried by the gas passing out of the reaction zones to be deposited on the walls of gas passages whereby much difficulty is caused by clogging of such passages. The water vaporized to control temperatures is produced. Such moisture tends to condenseon the dry lime produced when it cools and causes the residue to become moistened excessively.

By the present invention there is provided a method of generating acetylene which overcomes by-dropping water on a the reacting chosen in. the 3 time obtain a 40 Considerable quantities of dust are carried by the acetylene these and other dimculties. It has been discovered that freshly produced warm and dry calcium hydrate powder may be maintained in a very free flowing and fluid-like condition and that particles of carbide, being relatively heavier may be caused to fall down through a body of such hydrate. These properties are utilized in carrying out the present method of generation whereby carbide is fed into a reaction chamber into which controlled amounts of water are introduced and in which is maintained a body mixture of calcium hydrate in the desired fluid-like condition. The carbide and water react, forming acetylene and more hydrate. The carbide introduced, together with the newly-formed hydrate cause an upward displacement of the body of hydrate while the gas produced passes upward through the body of hydrate to assist in maintaining its fluid-like condition. At the top of the reaction chamber the excess hydrate over-flows and is withdrawn from further contact with gas which is collected above the reaction chamber and withdrawn to a gas holder. The contents of the reaction chamber are preferably continuously agitated by mechanical means to accelerate the reaction, to insure complete contact of carbide with-water, to effect a classification of the materials so that carbide will flow downward and displace hydrate tions become impurities in the gas and tend to removed from further contact with the residue as soon as the residue leaves the reaction chamber where it was mantained at a uniform high temperature. The water is preferably added at the bottom of the reaction chamber and the zone of greatest reaction activity is maintained at this point. The carbide is caused to move downward toward the water while move upward away from the water. This feature provides that the greatest production of heat takes place in the zone where excess water is available to absorb such heat as latent heat of evaporation and the warm gas and vapor evolved is caused to pass upward through the hydrate in the chamber to maintain it at an even temperature and in the desired fluid-like condition.

The present method of acetylene production is also inherently more stable, tending to balance out irregularities in the feed of carbide and water. For example, if a temporary excess of carbide is fed to the reaction chamber, the carbide settles to the bottom and remains until reacted with water and does not fiow along to contaminate the dry lime product. If, on the other hand, a temporary excess of water enters the reaction chamber, it remains at the bottom until sumcient carbide reaches it. The stability is of reat advantage in practice.

Another advantage of the present process results from preventing the heavy particles of impurities, such as i'erro silicon, which are present in certain forms of commercial calcium carbide from being withdrawn with the dry residue so that the residue is not contaminated.

. Refering now to the drawings, and particularly conduit 28 to the conduit the hydrate is caused to to Fig. 1, the means for supplying carbide is. shown generally at A. The reaction chamber where generation of gas occurs is shown generally at B, and at C is shown means for collecting the dry residue. Means for supplying water to the reaction chamber is-shown generally at D. The-reaction chamber in this form of the apparatus comprises the lower portion In of a closed generator casing H. The portion i0 is substantially cylindrical and its upper end joins an enlarged portion of the casing l2 wherein the gas produced separates from the particles of residue. The gas produced is let off the top of the enlarged portion l2 through a conduit l3, which connects to the pipe line H that conducts the gas to storage means, such as a gasometer. which is not shown in the interest of clearness of the drawing. At the upper part of the portion l0, there is connected the discharge end of a conveyor housing i5 within which is disposed a screw conveyor l6 which is rotated to feed carbide at a desired rate into the chamber In. The grade of carbide used in this form of the apparatus is preferably granular or lump form, the particle size being that adapted to be conveyed by conveyor l6. Disposed above the carbide conveyor is a carbide storage hopper I! which is connected to the conveyor housing i5'by a conduit III which has-an enlarged portion I! that provides additional storage space for carbide that per I1 is provided with a valve device 20 for shutting oi! the fiow of carbide when desired. A handle 2| is provided for moving the slide gate within the valve 20. For filling the hopper, there is provided a removable lid 22.

Water is introduced into the reaction chamber, preferably at a. point 23 close to or at the bottom of the chamber Ill. The water supply is provided throughthe conduit which is controlled by the valve 25 and which has interposed therein a metering orifice 26. Means for indicating the rate of flow of the water through the orifice is provided by a mercury-containing manometer 21 which has one leg connected by 24 on the downstream side of orifice 26 and the other leg connected by conduit 29 to conduit 24 on the upstream side of the orifice 26. These two conduits are provided 50 with stop valves 30 and 3| for disconnecting the lime storage hopper 35 with which it is connected by a connection 36. The conduit 34 is preferably provided with a spiral conveyor 31 which insures the desired movement of the residue. The lower portion or the lime storage hopper 35 is provided with an outlet 38 which is'controlled by a carry excess moisture out of the hydrate.

For insuring the proper agitation of the contents of the reaction chamber, there are provided .Iust. above the reaction two setsof agitators, both of which rotate about the central vertical axis of the casing ll. One agitating device comprises a frame 40 which is formed to closely follow the interior surface of the casing ll, there being two similar portions 40 which are joined at their upper and lower ends by arms 4| and 42 respectively. Thearm 4| is provided with a centrally located hub 43 which is keyed to the vertical inner shaft 44. This inner shaft is journaled at its upper end in a bearing 45 which is supported within the portion [2 of the casing by means of a threelegged brace 46 whose arms are attached to the walls of the casing. The lower end of the shaft 44 is journaled' in "a bearing 41 externally of the casing Surrounding the shaft 44, there is plrovided a hollow shaft 48 which passes up through a stufling box 49 in the bottom of the chamber l and to which are fastened a plurality of paddles or agitator blades 50 which are distributed throughout the full length of the chamber Ill. The shaft 44 is free to rotate within the shaft 48 and both shafts are preferably caused to rotate in opposite directions. The rotation is effected by means of a pair of bevel gears. The lower gear of. the pair is keyed to the inner shaft 44, while the upper gear 52 is kyed to the outer hollow shaft 48. Both gears 5| and 52 intermesh with a pinion 53, which, when rotated, causes the gears 5| and 52 to turn in opposite directions. Pinion 53 is mounted on the power outputshaft 54 of a speed changing gear box 55. The gear box 55 is also arranged to reduce the speed of its input power shaft 56 to the speed desired for normal operation. The shaft 56 is directly. connected .to an electric motor 51 which is supplied with electric power through the connection. 58. Interposed in the electric power supplyzline is 2. watt meter 29, which continually indicates the power being consumed in the operationof the generator. To provide space for the gearing underneath the casing, the casing is supported upon legs 6|]. The arm 42 is also provided with a central hub which is freely journaled upon the shaft 48 so that the scraper 40 may rotate in the opposite direction from the paddles or blades 50. The rotation of the two agitating systems in opposite directions provides for thorough agitation of the contents of the reaction chamber and is particularly effective for preventing the materials from bridging across between paddles. Near the bottom of the reaction chamber, there is provided an opening 6| for use in removing an accumulation of heavy particles of impurities, such as ferro-silicon. Theopening 6| is closed by a quickly removable cover 62. a

Means for indicating the temperature of the contents of the reaction chamber and of the gas produced are preferably provided. At 63 there is provided a thermometer having its temperature sensitive portion in contact with the interior of the reaction chamber at a point near the bottom thereof. The gas temperature is indicated by a thermometer 64 which has a temperature bulb projecting into the outlet conduit H. To prevent cooling and condensation of moisture that v is carried by acetylene that may come in contact layer of heat with the walls of easing portion l2, conveyor 34, and hopper 35, such parts may be covered by a insulation so that they are maintalned at a temperature above the condensation point.

The operation 0 the apparatus shown in Fig. 1

is as follows: A charge of carbide, preferably in- 34 and the conveyor 31 may contact with water until it has lump form, is placed in the hopper l1 and the lid 22 closed tight. Valve 20 is openedas by pulling the handle 2| outward'andihe conveyor I6 is rotated at a uniform ,rate. The electric motor 51 is simultaneously started up to set the agitator system in motion. When carbide starts feeding into the reaction chamber III, the valve 25 is opened a sufficient amount to supply water at the proper rate. The carbide and water react in the lower portion of the chamber Ill and. form calcium hydrate which is displaced upward, since the particles of hydrate are lighter than the particles of carbide. If the flow of water is not suflicient to react the carbide at the rate at which it is introduced, there will be an accumulation of excess carbide in the bottom of the reaction chamber Ill. The heavy carbide will impede the movement nf the agitator blades and more power will be consumed in turning them. The increased power consumption will be shown by the electric watt meter 59. This will indicate to the operator that the supply of water should be increased. However if too much water is added, the contents of the reaction chamber becomes heavier and less fluid-like so that the power required to turn the agitators again increases giving an immediate indication that the supply of water should be decreased. Observations of the temperature and of the moisture content'of the calcium hydrate indicate how the water supply should be controlled, but changes in these factors occur a certain period of time after a change in water supply rate.

When the reaction chamber ill fills with hydrated lime, it will reach the level of the-conduit then be rotated to remcre the hydrated lime produced. As the carbide is fed into the reaction chamber, it'rapidly falls down through the hydrated lime and in so doing it tends to remove any excess moisture therein. Carbide does not come actively into fallen to a point near the bottom of the reaction chamber and there the zone of greatest activity is found. The thorough agitation provided by the blades 40, 42, and 50 causes a thorough and intimate mixing of the water and carbide so that the hydrated lime that forms on the surface of each lump of carbide is immediately rubbed oil and is free to flow upwardly. As-the agitated mass of carbide reacts, a mechanical separation of the calcium hydrate and carbide occurs, the larger particles of unspent carbide sinking to the bottom of the generator while the fine particles of hydrate accumulate at the top of the agitated mixture. The heat of the reaction that occurs in the reaction zone is greater than can be carried away as sensible heat in the products of the reaction, by heating up to temperature the materials introduced and by heat loss to the external surroundings. Therefore to carry off this excess heat, an excess of water is supplied, preferably in the zone where the greatest amount of heat is produced. This excess water absorbs a considerable quantity of heat when changing from the liquid state to the vapor state and the vapors produced escape withthe gas. The volume of the hot gas generated is augmented'by the water vapor and v hydrated lime assists in maintaining the lime in a fluid-like condition.

With proper control of the rates of feeding the I carbide and water, a very finely-divided product ing for the purpose of reducing the velocity of the gas to a slow rate so that the fine particles of hydrate will not be carried along with the gas. The gas is thus separated from the hydrate before any appreciable cooling takes place so that the moisture which is carried by the gas does not have a chance to be condensed on the hydrate. The gas leaving the generator through conduit may be conducted through a dust separating means, such as a water scrubber to remove traces of dust that may be carried along, and simultaneously the gas may be cooled to normal temperature.

The apparatus shown in Fig. 2 is similar to that shown in Fig. l, but in this form of the apparatus the carbide is fed into the reaction chamber B near the bottom thereof from the carbide supply means which is shown generally at A. In this form of the apparatus, the reaction chamber 18 is conical in form, the bottom being smaller in diameter than the top. Such shape provides for more eflicient operation, for the'velocity of flow of the products upward decreases as the cross section of the reaction chamber increases. The upper chamber H in this embodiment com prises an open top tank having a. bottom 12 through which. the reaction chamber 18 passes centrally and which is Joined to the outer walls of the reaction chamber on a line substantially midway between the top and bottom of the reaction chamber. This construction forms an annular lime collecting space or compartment 18 surrounding the upper part of the reaction chamber. At a point near the top end of the upper chamber, there is provided an annular open top chamber 14 outside of the tank H which has a closed bottom that is welded to the side of the tank 1 I. Outside of the annular chamber 14 is disposed an annular water seal chamber. 18 having a closed bottom 11 that is welded to the side of.chamber 14. A sheet metal cover 18 for the tank 1| is provided having a depending cylindrical skirt portion 18 that extends down into the water seal 18 to a point close to the bottom 11 thereof. The cover 18 is formed higher in the central portion so that moisture that may condense thereon will flow to the edges and run down into the seal 16. The top of the water seal 18 is closed by an annular ring 88 which is welded to the upper edge of the seal 16 and to the upper portion of the skirt 18. An apron or bailie 8| surrounds the upper edge of the tank 1I in order to prevent particles of lime from falling down into the annular chamber 14. The lower edge of the skirt 18 is serrated, as shown at 82, for the purpose of providing an even distribution of gas that flows under the edge of the skirt 19 through the water seal. The water seal 18 thus constitutes an integral annular scrubber for the gas produced. This construction forms the subject matter of United States Patent 2,189,762, granted February 13, 1940, to Maurice O'Brien.

The agitating mechanism in this form of the apparatus is also provided with portions that rctate in opposite directions. In this case; however, the outer hollow shaft 88 does not extend through the reaction chamber but ends at a point just within the bottom 84 of the reaction chamber 18.

conical wall of the reaction chamber 18 and their upper ends, which extend just above the upper edge of the reactionchamber, are joined by a horizontal cross member 88. .The member 88 is so long as to almost touch opposite portions of the wall of the tank 1|. Secured to each end of the cross member 88 are two vertical scraper bars 88. These bars follow closely the cylindrical wall of the tank H to prevent any adherence of lime thereon. The bars 88 extend slightly above the edge of the tank H where they are joined by an upper cross member 88- whose ends extend to within a short distance from the cylindrical wall of the skirt 19. As best shown in Fig. 4, the members 88, 89, and 98 are maintained in the desired relation by two X-shaped cross frames 9| and 92 whose ends are welded to the members 88 and 98. Hollow hubs are provided at the central portion of each of the members 85, 81, 88, and 88. These hubs have bores which freely rotate upon a shaft 88 which passes axially through the generator in the vertical direction. Scrapers for stirring the lime that collects in the annular chamber 18 are provided by the depending bars 84 whose lower ends are joined to the lower ends of the vertical members 88 by cross bars 85 and whose upper ends are welded to the cross .member 88. Means is also provided for stirring the water in the scrubber water seal 16. This means'comprises two pairs of vertical bars 88, each pair fastened to opposite ends of the member 88 and having their lower ends attached to a horizontal scraper 91 which closely follows the bottom 11 of the water seal.-

The hollow shaft 88 projects through a sealing means 88 which is in the bottom 84 of the reaction chamber. The portion of the shaft 83 which extends below the bottom 84 is keyed to a bevel gear 99 that meshes withone of a pair of pinion bevel gears I88 that is mounted on the power output shaft I8I of a speed reducer I82. The long vertical inner shaft 93 has its lower end journaled in a bearing I83 which is in the bottom of a gear box I84 that fully encloses the bevel gears and which is fastened to the bottom 84. Another bevel gear I85 is keyed to the shaft 98 and meshes with the other of the pinions I88 so that the shaft 98 may be driven in an opposite direction and preferably at a slightly greater speed than the shaft 83. On the portion of the shaft 98 that passes through the reaction chamber 18. there is mounted a plurality of paddle blades I88 at points intermediate between the cross members 81. Both blades I86 and 81 may be arranged toprovide an upward or downward thrust on the materials being stirred in order that the agitation of the materials may be more thorough. It is generally preferable to provide an upward thrust so as to avoid packing and keep the materials in a looser condition. Also fastened tothe shaft on the upper side of the hub of cross member 88 is a set collar I81 which prevents upward shifting of the hub, and on either side of the hub of the cross member 90 there are also provided a pair of set collars I08. The shaft I 93 is journaled at its upper end in a bearing I that is mounted in the cover I0. The upper end of the shaft 93 is also provided with a re duced portion I I0 which passes through a stuihng box at the top of the bearing where it is provided with a cross arm bell strike III. The strike II I is arranged to ring-a bell I I2 twice upon each revolution of the inner paddle assembly. The bell is for the purpose of notifying an operator that the paddle assembly is rotating properly. Another alarm bell is provided to indicate that the outer paddle assembly carrying the scrubber scraper 91 is operating properly. To this end one of the scrapers 91 is provided with a vertical arm I I3 which strikes a depending portion of one end of the bell shaft 4 so as to tilt the bell mounted on the other end and cause it to ring once upon each revolution of the scraper. The shaft. II4 passeshorizontally through aseal bearing in the cylindrical outer wall of scrubber chamber IS.

The carbide is introduced at a point close to the bottom 84 of the reaction chamber I0 by through a stufling box I24 in the end of the housing H8 and has an outer end which is joumaled in the top bearing carried by the bearing support I25. A gear I25 is'mounted on the shaft I20 between bearing I25 and stuiilng box I24. The gear I26 is driven by an intermediate gear I21 which is mounted on a countershaft I20. The intermediate gear in turn is driven by a gear I20"which is mounted on the shaft MI. .The countershatt I28 has its ends journaled in a bearing in the bearing stand I25 andin a-bracket bearing I00 which is mounted in a support that extends from the underside-of the housing III. Another and I larger intermediate gear I3I is also mounted on the shaft I28 and a corresponding smaller gear I32 is mounted on the shaft IOI in such a way that it may be shifted into engagement with the gear I3 I or out of engagement therewith as desired; The gear I29 may alsobe shifted along the shaft .IOI so that the countershait I28 may bedrlven by either gear I29 or gear I02. Since the gears I29 and I32 are of different size, the shaft I28 and conveyor IIS will be driven at different rates of speed according to the gear ratio selected. Rate of feed or carbide may thus be varied as de sired to change the rate of gas production.

The shaft IOI passes through the lower bearing in the bearing stand I25v and is connected to the output side 'of the speed reducer I02 which isdriven by the electric motor 51. A stufllng box I33 is provided at the point where shaft 'IOI passes through the gear, housing I04 so that the gear housing may be maintained substantially filled with gear lubricant.- This seal also tends to prevent material ijrom passing from the reactionchamber through the seal "98.

Since certain grades of' commercial calcium carbide are relatively impure and contain such heavy impurities as silicon carbide, ferro-silicon, and oxide of iron and aluminum, means is provided for removing such, impurities. Removal of such impurities that may collect in the bottom of. the reaction chamber I0 is provided by a valve device I34. This device comprises a cylindrical bore formed in the bottom 84, within which is fitted a rotatable sleeve I35. The bore has an 5 opening I30 communicating with the chamber I0 and the sleeve I35 has a corresponding opening III in its wall which may be made to register with the opening I30 so that heavy particles that collect on the bottom of the chamber I0 will be 10 swept around by the arm 85 so as to fall through the openin s I36 and I31 into the chamber within the sleeve I05. When the sleeve is filled with such particles, it is rotated-so that the opening to chamber I0 is closed ctr and then the cover 15 I38 may be removedand the impurities taken out of the sleeve chamber without further loss or material from the chamber I0. The handle I00 is used to rotate the sleeve I35 while the cover I30 is in the closed position.

- 20 The substantially dry residue produced which collects in the annular compartment I3 is moved around by the arms 05 so that it tails through an 7 opening I40 located in the bottom I2 of the tank II. A receiving chamber MI is connected im- 25 mediately below'the opening I40 so as to receive the residue. The lower end of chamber I4I communicates witha lime conveyor I42 that withdraws the hydrated lime that collects in chamber I and deposits it in astorage hopper which is not shown in the-drawings. To prevent gas from passing out through the opening I40, chamber I, and conveyor I42, 'a dust seal is maintained in the chamber I. This seal is provided by maintaining a supply or the dry hydrate m the 35 lower part of the chamber. To determine the amount oi residue collected in. the chamber I4I, there is provided an indicating means vin the form of a rod I40 having at its lower enda disk I44 and at its upper end a handlel. 'I'he'rod 40 passes through the top of the chamberI 4| through a stuiilng boar I46 and by moving the rod I4lup and down the height or the lime in the chamber may be readily determined. The operation of the conveyorI42 is so controlled that a supply of lime 5 is caused to remain in .the lower part of the chamber I 4Isoastomaintainthe seal.

The water required for the reaction .and for absorption of excess heat is added atpoints I" close to the bottom of the The. rate or flow or the water supply may be determined by means o'i-a flow meter comprising an orifice-26 and'manometer' 21 as shown in Fig. '1 or by any means for maintaining a. regulatable constant supply of water such, for example, as. a posi- 55 tive displacement pump whose speed of operation may be regulated. I! desired, water for initially contacting the carbide being supplied to. the reaction chamber may be introduced vthrough a conduit I48 which-is connected to the conveyor 60 housing II0.

A supply of waterisladded to the scrubber seal I6 through the connection I40 which is located in the cover of the seal. Excess water normally flows out of the seal through the gas outletpipe 65 I50 which is connected to theI-outer wall of the seal I0 at a desired point. This overflow water nmsalong the conduit I50 untiiit reaches a draining conduit depending therefrom or any desired water operating means. The annular cham 70 ber I4 is provided so that water; which might be driven backward by an abnormal backflow of gas through this scrubber will be caught by the chamber I4 instead of being carried into the tank II.

To remove water that may reach the chamber I4, 75

reaction chamber I0. 50

there is provided a drain conduit l5! connected to the lower part of the chamber 14 and depending down into a water seal I52. The depth of the seal IE2 is suiilcient to provide a. head of water greater than the normal pressure of the gas in the generator. The water seal I52 is provided with an overflow drain I53 and a vent pipe I54, both connected to the upper portion thereof.

The operation of the form of apparatus shown in Fig. 2 is similar to that of Fig. 1. In this form, however, calcium carbide of any form may be used, that is, lump, dust, or run-of-crusher sizes, the maximum size of the lumps being limited to that which can be conveyed by the feeding device. The very fine particles of carbide introduced into the reaction chamber 10 are heavier than the calcium hydrate and therefore tend to remain in the chamber to be converted into acetylene and hydrate. The larger particles, of course, settle more rapidly and remain at lower levels in the chamber where greater moisture is available for reacting them. I I

The carbide is fed into the chamber 10 by conveyor H5 at a substantially constant rate determined by the gear ratio of the gears I21 and I29, or "I and I32 selected. The water is introduced at a constant rate which is regulated according to the temperature and the moisture content of the lime product. This rate must be maintained despite variationsin back pressure at the water I inlets which may occur due to particles being pressed against the inlets. It is therefore preferable to have a plurality of such inlets, and, to maintainv the flow constant, the water may be supplied from a high pressure source and a differential pressure regulator interposed in the pipe line or a positive displacement pump whose speed or volumetric displacement are regulatable may be employed. A portion of the water for initially contacting the carbide may be added if desired in the conveyor H8 through inlet connection I48 3: just as the carbide enters the reaction cham- Rotation of the paddle assemblies keeps the mixture of carbide and hydrate in the reaction chamber thoroughly'agitated while the gas and vapor flowing upward assist the agitation and tend to make-the-hydrate more fluid-like. The

carbide particles remain in the chamber in until consumed'but the hydrate overflows the top of the chamber "Ill and falls into the annular compartment I3. Here the hydrate is stirred and swept around by the scrapers 88 so as to fall through opening 0 into the hopper I at a rate such as to maintain a plug of hydrate in the bottom of the hopper so that gas will not escape to the conveyor I42. Anyother means for effect- 8 a gas seal while withdrawing the hydrate might be used. The calcium hydrate may be stirred for an additional period'in the compartment 13 if desired by providing the outlet for ydrate in the side wall ll instead of in the bottom at opening I. Such additional stirring will tend to produce a more uniiorm product.

The acetylene and water vapor are released at the top of the reaction chamber into the relatively large space above, formed by the tank II and cover 18. In this space the velocity of flow is so reduced that the liner particles of hydrate settle down and the gas flows over the upper edge of tank ll, down between skirt l9 and chamber wall 14 and up throughthe water in the space between skirt l9 and seal wall 16. The serrations 82 cause the gas topass in very small bubbles which provide thorough contact with the water in the seal which consequently removes the last traces of hydrate and cools the gas to a desired temperature. A substantial portion of the vapor carried by the gas is condensed and flows oil with the overflow water of the seal.

When first starting up the generator, the motor 51 is started, water is admitted to the scrubber at inlet Band the carbide valve I I! opened. When carbide enters the chamber 10 admission of water is begun. When shutting down the generator, the carbide valve 9 is first shut oil, the water is allowed to enter for a specified period of time and is then shut oil. and thepaddles are kept turning for an additional period to insure that the moisture is evenly distributed and dispersed. The generator may then stand idle for a period without danger of lime caking in the reaction chamber.

Ithas been found that when the water supply is properly regulated in accordance with the rate of supply of carbide and the degree of agitation,

' the maximum temperature reached in the reaction zone in chamber Ill may be maintained at ate d as described, a hydrated lime product having a residual moisture content of about 3% was obtained when a ratio of 1 lb. of water to 1 lb. of carbide was maintained. This ratio willvary slightly according to the purity of the carbide used. Such a moisture content is desired in commercial lime hydrates for then the handling properties of the material are best. It is therefore seen that the process of the present invention provides for the production of acetylene at relatively rapid rates from carbide and the simultaneous production of a high quality commercially useful hydrated lime lay-product.

We claim: I I

1. Process for producing a gas and a substantially dry residue by the action of a solid and a liquid, which comprises bringing controlled amounts of said solid and said liquid into contact in a reaction zone thereby forming a mixture of reacting materials, said amounts being proportioned so as to complete the reaction to form a substantially dry residue and said gas, and said liquid being introduced into the lower portion of said reaction zone: agitating said mixture to cause selective upward movement within said mixture of said residue by the displacing action of said solid to move said residue out of said reaction zone; causing said solid to be retained in said reaction zonefor complete conversion; and separately collecting the gas and the substantially dry residue.

2. In a process for producing a gas and a substantially dry residue by the reaction of a solid and a liquid, the steps comprising bringing controlled amounts of said solid and said liquid into contact in the lower part of a reaction zone thereby forming a mixture of reacting materials, said amounts being proportioned so as to complete the reaction to form a substantially dry residue and said gas, agitating said mixture to .tact in a reaction zone and .and said liquid being introduced cause upward movement within said mixture of the gas and residue products to a point out of said reaction zone by the displacing action of said solid, retaining said solid in said reaction zone until completely reacted, and separately withdrawing the gas and substantially dry residue.

3. Process for producing a gas and a substantially dry residue by the reaction of a solid and a liquid, which comprises bringing controlled amounts of said solid and said liquid into conthereby form a mixture of reacting materials, said amounts being proportioned so as to complete the reaction to form a substantially dry residue and said gas, into the lower portion of said reaction zone; retaining said solid in said reaction zone until completely reacted; continuously agitating said mixture and withdrawing the gasproduced from the upper portion of said reaction zone, so as to maintain said residue in ailuid-like conditionand float said residue up ardly out oi said reaction zone by the displac g action of said solid and the buoyant effect of the upward passage of said gas; and separating said gas from said residue and separately collecting said residue.

4. Process for producing. a gas and a substantially dry residue by the exothermic reaction of a solid and a liquid which comprises, bringing controlled amounts of said solid and said liquid into contact in a reaction zone thereby forming a mixture of reacting materials, said amounts being proportioned so as to complete the reaction to form a substantially dry residue and said gas and atleast the major portion oisaid liquid being introduced near the bottom of said reaction zone, retaining said solid in the reaction zone until completely reacted, controlling the temperature of said reaction zone to below a desired upper limit by introducing additionally a suflicient quantity of liquid not required for completing the reaction for absorbing by its evaporation the excess heat 0! the reaction, removing the vapors so produced with the gas generated, agitating said mixture to promote the flow of the products of the reaction together upwardly out of the reaction zone by the combined displacing action of the incoming solid and the buoyant action of the generated gas, separating the gas and vapor from the residue] and separately collecting the substantially dry residue and withdrawing the gas and vapor.

5. Process for producing a gas and a substantially dry residue by the exothermic ,reaction of a solid and a liquid-which comprises bringing controlled amounts of said solid .and said liquid into contact in a reaction zone near the lower end thereof and thereby forming a mixture of reacting materials, said amounts being proportioned so as to complete the reaction to form a substantially dry residue and said gas: retaining said solid in the reaction zone until completely reacted; agitating said mixture to accelerate stantially dry residue by the exothermic reaction of a solid and a liquid, which comprises bringing controlled amounts of said solid and said liquidinto contactin the lower portion of a reaction zone thereby forming a mixture of re-. acting materials, said amounts being proportioned so as to complete the reaction to form a substantially dry residue and said gas; retaining said solid in the reaction zone reacted; controlling the mean temperature of said reaction zone to a value below a safe upper limit by introducing additionalquantities of a liquid-sumcient fort absorbing by its evaporation the excess heat of reaction, and removing the vapors so produced with the gas generated: agitating said mixture to accelerate the reaction and substantially equalize the temperatures locally attained in the reaction zone, and also to promote the flow of substantially dry residue upwardly and out of the reaction zone by the combined displacing action of the solid and the buoyant action or the generated gas; separating the gas and vapor from the residue; and separately collecting the substantially dry residue and withdrawing the gas and vapor.

'7. Process for reacting a solid and a liquid for until completely producing a gas and a substantially dry residue 3 cumulating in said chamber. a mixture comprisliquid being introduced near the lower end 01' said reaction chamber, ac-

ing said solid and residue, agitating said mixture to cause movement of said solid toward the point of feeding said liquid and movement of said residue countercurrently with respect to said solid and away from said point, and separately collecting the gas and the residue;

8. Process for reacting a solid and a liquid for producing avgas and a substantially dry residue,

which comprises introducing said solid into a reaction chamber; introducing controlled amounts of said liquid into the reaction chamber near the bottom thereof so as to contact said solid and produce said gas and a substantially dry residue; accumulating in said chamber a mixture com prising said solid and residue; agitating said mix- ,ture so as to effect a classification of the components thereof whereby the relatively lighter residue component is displaced upwardly by the heavier solid component; withdrawing said residue from the upper portion 01' said mixture; and

separately withdrawing the gas.

9. Process for reacting asolid and a liquid for producing a gas and a substantially dry residue which comprises, introducing said solid into a reaction chamber at a point abovethe bottom thereof, introducing controlled amounts of said liquid at a point below the point of introduction of the solid, accumulating in said chamber a mixture comprising saidsolid and products of reaction including the substantially dry residue, agitating said mixture to cause movement of said solid ina downward direction within the mixture to contact and react with liquidintroduced and be converted into gas and residue, maintaining said residue within said mixture in a substantially fluid-like condition, causing said residue, by

the displacing action of said solid, to flow upwardly within said mixture and to flow over the top of said reaction chamber, and separately. withdrawing the gas and said residue in a substantially dry condition. v

10. Process for reacting asolid and a liquid for producing a gas and a substantially dry residue which comprises, introducing said solid into a reaction chamber at a point above the bottom thereof, introducing controlled amounts of said liquid at a point below the point of introduction of the solid, accumulating in said chamber a mixture comprising said solid and products of reaction including the residue, causing said gas to flow upward through said mixture to maintain the residue in a fiuid-like condition, continuously agitating the components of said mixture to effect improved contact of said solid and liquid, to accelerate the reaction, and to' cause counterflow of solid downward and residue in an upward direction, continuously removing residue from the'upper portion of said chamber, collecting and removing particles of unreacted material from the lower portion of said chamber and collecting and withdrawing said gas from above said chamber. l

11. Process of continuously producing acetylene and substantially .dry calcium hydroxide fromcalcium carbide which comprises, continuously agitating a substantially dry mixture comprising calcium carbide and calcium hydroxide so as to efiect-a classification by gravity of the constituents thereof continuously adding limited amounts of water to the lower portion of said mixture, continuously adding calcium carbide to said mixture in amounts suflicient to replenish that reacted, and continuously removing substantially dry calcium hydroxide product from the upper portion of said mixture.

1 12. Process of continuously producing. acetylene and substantially dry calcium hydroxide from calcium carbide which comprises, continuously agitating a substantially dry mixture comprising calcium carbide and reaction products so as" to efiect a classification of the constituents thereof, continuously adding limited amounts of water to the lower portion of said mixture, the amount of water employed being not more than that necessary to effect conversion of the calciumcarbide into acetylene and calcium hydroxide and to absorb by evaporationsuil'lcient of the.

'eat ,of reaction to maintain the temperature below a safe predetermined limit, continuously adding calcium carbide to said mixture, and continuously removing substantially all the dry calcium hydroxide from the upper portion 01' said mixture.

13. Process of continuously producing acetylene and substantially dry calcium hydroxide from calcium carbide which comprises, continuously agitating a mixture comprising calcium carbide and reaction products so as to eflect a classification of the constituents thereof, continuously adding limited amounts of water to the lower portion of said mixture, the amount of water employed beingnot more than that necessary to effect conversion of the calcium carbide into acetylene and calcium hydroxide and to absorb by evaporation sufiicient oi the heat of reaction to maintain the temperature below a sate predetermined limit, continuously adding calcium carbide to said mixture, causing the acetylene and vapors generated to pass upward through said mixture so as to maintain the calcium hydroxide in a fluid-like condition and to promote said classification, separating said acetylene and vapors from the calcium hydroxide above said mixture and, continuously removing substantially all the dry calcium hydroxide from the upper portion of said mixture.

14. Process of continuously producing acetylene and substantially dry calcium hydroxide its evaporation excess heat from calcium carbide which comprises, continuohsly agitating a mixture comprising calcium carbide and calcium hydroxide so as to eiiect a classification of the constituents thereof, contln-- uously adding limited amounts of water to the lower portion of said mixture, the amount of water employed being not more than that necessary to eirect conversion of the calcium carbide into acetylene and calcium hydroxide and to absorb by evaporation suflicient of the heat of reaction to maintain the temperature below a safe predetermined limit, continuously adding calcium carbide to said mixture, causing the acetylene and vapors generated to pass upward through said mixture so as to maintain the calcium hydroxide in a fluid-like condition and to promote said classification, separating said acetylene and vapors from the calcium hydroxide above said mixture and continuously removing substantially dry calcium hydroxide from the upper portion of said mixture, and collecting and removing relatively heavy particles of unreacted material from the lower portion of said mixture.

15. Process for producing acetylene and subreaction zone by the displacing action of said can A bide; retaining said carbide in said reactionzone until substantially completely reacted: and withdrawing the acetylene from the reaction zone and separately collecting the substantially dry hydrate.

16. Process for producing acetylene and substantially dry calcium hydrate irom calcium car bringing cgntrolled bide, which comprises amounts oi. calcium carbide and water into intimate contact near the lower-end or a reaction zone thereby forming a mixture of reacting materials, said amounts being proportioned so as to i'orm acetylene and a substantially dry hydrate: retaining calcium carbide in the reaction zone until completely reacted; maintaining the hydrate in a fluid-like condition by passing acetylene therethrough; agitating said mixture to promote the ilow oi said hydrate out of said reaction zone'by the combined displacing action or the carbide and the buoyant action of the generated gas; separating the acetylene from said hydrate: and separately withdrawing the acetylene and said substantially dry hydrate.

17. Process for producing acetylene and substantially dry calcium hydrate irom calcium car- 'bide, which comprises bringing controlled amounts oi calcium carbide and water into intimate contact in a reaction zone thereby forming a mixture of reacting materials, said amounts being proportioned so as to form acetylene and a substantially dry hydrate, and said water being introduced into the lower portion 01 said reaction zonerretaining calcium carbide in the reaction zone until completely reacted; controlling the mean temperature or said reaction zone to a value below a desired sai'eupper limit by introducing additional water sumcient for carrying away by 01' reaction, and removing vapor so produced with the acetylene lenerated; agitating the mixture of reacting materials to accelerate the reaction and substantially equalize the temperature locally attained in the reaction zone, and also to promote the flow oi the products of reaction out of the reaction zone by the displacing action of the carbide; separating the acetylene and vaporirom the hydrate; and separately collecting the substantially dry calcium hydrate and withdrawing the acetylene and vapor.

18. Process for producing acetylene and substantially dry calcium hydrate from calcium carbide which comprises bringing controlled amounts of calcium carbide and water into intimate contact in the lower portion of a reaction zone, accumulating in said zone a mixture comprising said carbide and substantially dry calcium hy drate product of the reaction, mechanically agitating said mixture to promote classification of the constituents thereof and displacement of hydrate out of said zone by the displacing action of the incoming carbide, subjecting the hydrate displaced from said zone to additional agitation so as to improve the quality of the calcium hydrate product and separately withdrawing acetylene and calcium hydrate.

19. Process for producing acetylene and sub stantially dry calcium hydrate from calcium carbide which comprises feeding calcium carbide into a reaction chamber at a point above the bottom thereof, adding limited amounts of water at a point below the point of feeding the calcium carbide, accumulating in the chamber a mixture comprising calcium carbide and calcium hydrate, agitating said mixture to cause downward movement oi the calcium carbide so as to contact and react with the water introduced and be converted into acetylene and hydrate, maintaining the hydrate in a fluid-like condition, causing said hydrate to flow upwardly and concurrently with the acetylene by the displacing action of the calcium carbide promoted by the agitation of said mix-' ture, collecting and withdrawing the substantially dry calcium hydrate which rises to the top of the chamber, and separately collecting and withdrawing the acetylene from above said chamber.

20. Process for producing acetylene and substantially dry calcium hydrate from calcium carbide which comprises feeding calcium carbide into a reaction chamber at a point above the bottom thereof, adding limited amounts of water at a point below the point oi'teeding the calcium carbide, accumulating in the chamber a mixture comprising calcium carbide and calcium hydrate, causing the generated acetylene to flow upwardly through said mixture to maintain the hydrate component in a fluid-like condition, continuously agitating the components of said mixture to effect improved contact of the calcium carbide and water, accelerate the reaction and promote move.- ment of the calcium carbide downwardly so as to displace hydrate in an upward direction, removing substantially dry hydrate from the upper portion or said mixture, collecting and removing particles of unreacted impurities from the bottom of I said chamber, collecting acetylene above said chamber and cleaning said acetylene as withdrawn.

CHARLES mass.

CERTIFICATE OF CORRECTION. Patent No. 2,255,108. February 25, 1914.1.

CHARLES NESS, ET AL.

It is hereby certified that error appears in the printed specification of the above numbered patent requiring correction as follows: Page 2, first column, line 11, strike out the word "body"; line 67, for "The" read -Thls-; page 5, first column, line 59, for the reference numeral "29" read --59 page 5, second column, line "(0, for the word "operating" reed --separating; page 6, second column, l1ne'5l, claim 1, for "action". read -reaction; and that the said Letters Patent should be read with this correction therein that the seme may conform to the record of the cage inthe Patent Office.

Signed and sealed this 25th day of March, A. D. 19111.

Henry Van Aradale, (seal) Acting Commissioner of Patents 

